|Publication number||US6165431 A|
|Application number||US 09/286,829|
|Publication date||26 Dec 2000|
|Filing date||6 Apr 1999|
|Priority date||8 Dec 1993|
|Also published as||EP1183092A1, EP1183092A4, WO2000059613A1|
|Publication number||09286829, 286829, US 6165431 A, US 6165431A, US-A-6165431, US6165431 A, US6165431A|
|Inventors||Richard Mackay, Michael Schwartz, Anthony F. Sammells|
|Original Assignee||Eltron Research, Inc.|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (46), Non-Patent Citations (52), Referenced by (28), Classifications (86), Legal Events (9)|
|External Links: USPTO, USPTO Assignment, Espacenet|
Ax A'x A"2-(x+x') By B'y B"2-(y+y') O5+z
Ax Srx' By Fey' Co2-(y+y') O5+z,
Ax A'x' A"2-(x+x') By B'y' B"2-(y+y') O5+z
Ax A'x' A"2-(x+x') By B'y' B"2-(y+y') O5+z
The research for this invention was supported by a grant from the U.S. Department of Energy, Grant No. DE-FG03-96ER82215. The United States government may have certain rights in this invention.
This application is a continuation-in-part of U.S. patent application Ser. No. 08/639,781, filed Apr. 29, 1996 now U.S. Pat. No. 6,033,632, which in turn is a continuation-in-part application of U.S. patent application Ser. No. 08/163,620 filed Dec. 8, 1993 now abandoned, both of which applications are incorporated by reference herein in their entirety to the extent not inconsistent with the disclosure herein.
Strong incentives exist for the development of efficient processes for the separation of oxygen from gas mixtures, such as air. Low-cost production would enhance the availability of pure oxygen for a variety of industrial applications including its use in high efficiency combustion processes. There is significant potential for the application of solid state catalytic membranes to oxygen separation. This technology is presently limited by the ceramic materials that are available. New ceramic materials that exhibit higher oxygen flux and improved mechanical and chemical stability in long term operation for use in membrane reactors are of significant interest in the art.
This invention relates to mixed metal oxide materials that are particularly useful for the manufacture of catalytic membranes for gas-phase oxygen separation processes. Oxygen-deficient oxides of this invention are derived from brownmillerite materials which have the general structure A2 B2 O5. The materials of this invention maintain high oxygen anion conductivities at relatively low membrane operating conditions ranging from about 700° C. to 900° C. The metal elements at the B-site in the brownmillerite structure are selected to provide mixed ion- and electron-conducting materials and particularly to provide material that conduct oxygen anions and electrons. The materials of this invention have the general formula:
Ax A'x' A"2-(x+x') By B'y' B"2-(y+y') O5+z
x and x' are greater than 0;
y and y' are greater than 0;
x+x' is less than or equal to 2;
y+y' is less than or equal to 2;
z is a number that makes the metal oxide charge neutral;
A is an element selected from the lanthanide elements and yttrium;
A' is an element selected from the Group 2 elements;
B is an element selected from the group consisting of Al, Ga, In or mixtures thereof; and
B' and B" are different elements and are independently selected from the group of elements Mg or the d-block transition elements.
The lanthanide metals include the f block lanthanide metals: La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and Lu. Yttrium has properties similar to the f block lanthanide metals and is also included herein in the definition of lanthanide metals. A is preferably La or Gd, with La more preferred. Group 2 metal elements of the Periodic Table (also designated Group IIa) are Be, Mg, Ca, Sr, Ba, and Ra. The preferred Group 2 elements for the A' element of the materials of this invention are Ca, Sr and Ba and Sr is most preferred. The more preferred B elements are Ga and Al, with Ga more preferred. The d block transition elements include Sc, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, and Zn. Preferred B' and B" elements are Mg, Fe and Co, with Fe and Co being more preferred as B' and B", respectively.
Mixed metal oxides in which B" and B" are Fe and Co are particularly preferred for membranes having high oxygen flux rates.
The value of z in the above formula depends upon the values of x, x', y and y' and the oxidation states of the A, A', A", B, B' and B" elements. The value of z is such that the mixed metal oxide material is charge neutral. In preferred materials, 0<z<1.
Preferred stoichiometries for materials of this invention of the above formula are those in which x is about 0.1 to about 0.6, and x' is about 1.4 to about 1.9, and where in addition x+x' is about equal to 2. More preferred are materials in which x is about 0.3 to about 0.5 and x' is about 1.5 to about 1.7. Also preferred are those materials of the above formula where y is about 0.3 to about 0.9 and y' is about 0.70 to about 1.70. More preferred materials have y=about 0.6 and y'=about 1.0 to about 1.4. More preferred materials have y+y' equal to about 1.6 to about 2.0.
Electronically- and ionically-conducting membranes employed in the oxygen-separation reactors of this invention comprise mixed metal oxides of the above formula. Substantially gas-impermeable membranes having both electronic and ionic conductivity are formed by initially preparing mixed metal oxide powders by repeatedly calcining and milling the powders of individual metal oxides or the corresponding carbonates (or other metal precursors) in the desired stoichiometric ratios. The resulting mixed metal oxide is then pressed and sintered into dense membranes of various shapes, including disks and open-one-ended tubes. These membranes are then employed to construct catalytic membrane reactors, particularly for oxygen separation processes. The purity of the product oxygen produced in reactors of this invention, which can be stored or used in other chemical processes, is generally greater than about 90% and preferably greater than about 99%.
The presence of the mixed metal oxide of desired stoichiometry (as in the given formulas) in a repeatedly calcined and milled mixed metal oxide can be assessed by X-ray diffraction studies. Further, the presence of distinct phases of metal oxides or other metal species that may be present in the mixed metal oxides materials of this invention can be detected by X-ray diffraction techniques by the observation of peaks not assignable with the predominate mixed metal oxide of desired stoichiometry. The level of distinct phase material that can be detected depends upon the resolution and sensitivity of the X-ray diffractometer employed and upon the identity and number of the distinct phases present. It is believed that greater than about 4% by weight of another phase can be detected by the X-ray diffraction method employed (FIGS. 1-5)
A catalytic reactor of this invention comprises an oxidation zone and a reduction zone separated by the substantially gas-impermeable catalytic membrane which comprises the electronically and ionically conducting mixed metal oxides of the above formula. Once in the reactor, the membrane has an oxidation surface in contact with the oxidation zone of the reactor and a reduction surface in contact with the reduction zone of the reactor. Electronic conduction in the reactor is provided through the membrane material which is a mixed ion and electron conductor (i.e., conducts both electrons and ions, such as oxygen anions). A reactor also comprises passages for admission of oxygen-containing gas, such as air, into the reactor reduction zone and admission of an oxygen-depleted gas, inert gas or reduced gas into the oxidation zone of the reactor. A vacuum can alternatively be applied to the oxidation zone to remove separated oxygen from the oxidation zone. Oxygen removed in this way can be collected and concentrated, if desired. The reactor also has gas exit passages from the reduction and oxidation zones. A plurality of membrane reactors can be provided in series or in parallel (with respect to gas flow through the reactor) to form a multi-membrane reactor to enhance speed or efficiency of oxygen separation.
In operation for oxygen separation, an oxygen-containing gas, such as air, is introduced into the reduction zone of the reactor in contact with the reduction surface to the catalytic membrane. Oxygen is reduced to oxygen anion at the reduction surface and the anion is conducted through the membrane to the oxidation surface. At the oxidation surface, the oxygen anion is re-oxidized to oxygen which is released into the oxidation zone of the reactor. (Alternatively, oxygen anion can be employed to oxidize a reduced gas (e.g., a hydrocarbon gas) at the oxidation surface of the membrane.) Membrane materials of this invention conduct electrons as well as anions. (Membrane materials that also conduct electrons allow charge neutralization of the membrane during operation.) Gases in the reactor can be under ambient or atmospheric pressure or they can be placed under higher or lower pressure (e.g., a vacuum can be applied) than ambient conditions. During operation for oxygen separation, the membrane is heated typically at a temperature above about 700° C. and more typically from about 700° C. to about 1100° C. Preferred materials of this invention can be efficiently operated at temperatures that are generally lower than those currently used in the art, at from about 700° C. to about 900° C.
The oxidation surface, or the reduction surface or both surfaces (or parts of those surfaces) of the membrane can be coated with an oxidation catalyst or reduction catalyst, respectively, or both. A preferred catalyst for either or both surfaces of the membrane is La0.8 Sr0.2 CoO3-z where z is a number that makes the oxide charge neutral.
An oxygen flux of about 1 ml/min-cm2 or higher can be obtained through a 1 mm- thick membrane at ambient pressure and at an operating temperature of about 900° C. These high flux rates can be maintained for long-term operation, e.g., up to about 700 h of operation.
Membrane materials as described herein can be employed in a method for oxygen separation from an oxygen-containing gas. In this method a reactor, as described above, is provided with a substantially gas-impermeable membrane which separates an oxidation and reduction zone. Oxygen is reduced at the reducing surface of the membrane, the resulting oxygen anions are then transported across the membrane to the reduction surface where oxygen anions are re-oxidized to form oxygen which is released into the oxidation zone for collection. This method can be employed to generate high purity oxygen (greater than about 90% purity) or very high purity oxygen (greater than about 99% purity) or to generate oxygen-enriched gases (e.g., oxygen in an inert gas).
FIG. 1 is an x-ray diffractometer scan for calcined mixed metal oxide having the formula La0.4 Sr1.6 Ga0.6 Fe1.4 O5+z.
FIG. 2 is an x-ray diffractometer scan for calcined mixed metal oxide having the formula La0.3 Sr1.7 Ga0.6 Fe1.1 Co0.3 O5+z.
FIG. 3 is an x-ray diffractometer scan for calcined mixed metal oxides having the formula La0.4 Sr1.7 Al0.6 Fe1.1 Co0.3 O5+z.
FIG. 4 is an x-ray diffractometer scan for calcined mixed metal oxides of formula La0.4 Sr1.6 Ga0.6 Fe1.2 Co0.2 O5+z.
FIG. 5 is an x-ray diffractometer scan for calcined and sintered mixed metal oxides of formula La0.4 Sr1.6 Al0.6 Fe1.2 Co0.2 O5+z.
FIG. 6 is a graph of oxygen permeation (ml/min-cm2) at 900° C. as a function of time for compounds of composition Sr1.7 La0.3 Ga0.6 Fe1.4-y COy O5+z where 0.0≦y≦0.4. Closed circles (----) are the results with the composition where y=0, closed triangles (--▴--) are results where y=0.10, closed squares (--▪--) are the results where y=0.20, closed diamonds (--♦--) are the results where y=0.25, closed inverted triangles (--▾--) are the results where y=0.30 and open circles (--◯--) are the results where y=0.35.
FIG. 7 is a graph of oxygen permeation at 900° C. (ml/min-cm2) as a function of time for compounds of composition Sr1.6 La0.4 Ga0.6 Fe1.4-y Coy O5+z where 0.0<y<0.4. Closed circles (----) are the results with the composition where y=0.10, closed triangles (--▴--) are results where y-0.15, closed squares (--▪--) are the results where y=0.20, closed diamonds (--♦--) are the results where y=0.25, closed inverted triangles (--▾--) are the results where y=0.30 and open circles (--◯--) are the results where y=0.35.
Brownmillerites are generally referred to as having the formula A2 B2 O5. Brownmillerite is considered to be derived from the perovskite structure by removal of 1/6 of the oxygen atoms. Solid state compositions based on the brownmillerite parent compound Ba2 In2 O5 and useful in this invention are formed by introducing dopants or substitutents into the B-site of the lattice to lower the order-disorder phase transition. Higher oxygen anion conductivity is generally found to correlate with the disordered phase. Clear correlations exist between perovskite-related crystallographic and thermodynamic parameters with empirical parameters relating to the activation energy (Ea) for ionic transport. Lower values of Ea favor higher ionic conduction. The derived expression for ionic conductivity is given by:
where K is the Boltzman constant and -.increment.Hm is the enthalpy of activation which is equivalent to Ea. This equation indicates that the overall ionic conductivity σ is a function of both an exponential term and a pre-exponential term. The pre-exponential term, A is given by:
A=(Zλ2 e2 / 6νo K)C(1-C)νo exp(.increment.Sm / K)
where .increment.Sm is the activation entropy, C is the fraction of available sites occupied by mobile ions, A is the jump distance, Z is the number of jump directions νo is the molar volume and e is the electronic charge. The exponential term is related to the activation energy. These equations provide a rationale for dopant metal cation selection to improve ionic conduction. Dopants are selected to improve ionic conductivity by (i) optimizing vacancy concentration to maximize the pre-exponential term A, and (ii) decreasing activation energy to maximize the exponential term.
Membrane materials of this invention can be used for oxygen separation or oxygen enrichment, i.e., for decreasing the oxygen concentration in one gas stream and increasing or enriching the oxygen concentration in another gas stream. Oxygen-containing gas includes air, oxygen in nitrogen, oxygen in inert gases and contaminated oxygen. Oxygen from the oxygen-containing gas can be transferred in the reactors of this invention, in principle, to any gas in which it is desired to increase oxygen concentration, in particular an inert gas, nitrogen, a reduced gas (i.e., hydrocarbon-containing gas) can be introduced into the oxidation zone of the reactor. Alternatively, a vacuum or partial vacuum can be applied to the oxidation zone to collect separated oxygen. The separated oxygen can also be used to oxidize a reduced gas in the oxidation zone, i.e., to form oxygenated hydrocarbons.
This invention provides a method for separating oxygen from oxygen-containing gases and/or for oxygen enrichment of oxygen-deficient gases in which it is desired to increase the level of oxygen. The method employs a reactor having two chambers or zones (an oxidation zone and a reduction zone) separated by a substantially gas impermeable membrane. A substantially gas impermeable membrane may not be completely impermeable to small gaseous species such as hydrogen gas and may allow a low level of leakage of other gases. It is particularly important that the membrane be impermeable to gases from which oxygen is to be separated, such as nitrogen. Preferred membranes are formed without substantial cracking and gas leakage. The membrane is capable of transporting oxygen ions and also conducts electrons. The membrane is fabricated from an ion-conducting and electron-conducting mixed metal oxide of this invention having the formula given above.
The oxygen-containing gas is introduced into one chamber, the reduction zone, in contact with the reduction surface of the membrane. A differential oxygen partial pressure is established between the two chambers or zones, with oxygen partial pressure higher in the reduction zone. The differential partial pressure can be established by introducing an oxygen-deficient gas or a reduced gas into the oxidation zone which has a lower concentration of oxygen than in the oxygen-containing gas. The oxygen-deficient gas can be an inert gas such as helium. Alternatively, a partial or full vacuum can be applied to the oxidation zone to remove transported oxygen. Gas pressure in the zones may be ambient or higher or lower than ambient to achieve the desired differential oxygen partial pressure. The membrane is heated to a temperature that facilitates oxygen anion transport and also facilitates electron transport. Oxygen is transported across the membrane to enrich the oxygen content of the oxygen-deficient or reduced gas. Oxygen can be concentrated from the oxygen-enriched gas exiting the oxidation zone.
During operation the membranes of this invention are heated, typically to at least about 700° C. At lower temperatures, e.g., at 600° C., ionic conductivity of the 1 mm thick membrane is typically too low for practical operation.
The oxygen-separation reactors of this invention can be combined with other known methods for gas purification or gas separation to provide desired levels of purity in gas streams. The gas stream output of oxygen-separation reactors can be introduced as product gas streams for other reactors.
Mixed metal oxide materials useful for preparation of ionically- and electronically-conductive membranes include, among others:
______________________________________Ax Srx' By Fey' Co2-(y+y') O5+z particularly where x is about 0.3 to about 0.5, x' is about 1.5 to about 1.7, y is 0.6, y' is between about 1.0 and 1.4, and where B is Ga or Al. Lax A'x' By Fey' Co2-(y+y') O5+z particula rly where x is about 0.3 to about 0.5, x' is about 1.5 to about 1.7, y is 0.6, y' is between about 1.0 and 1.4, and where B is Ga or Al. Lax Srx' By B'y' Co2-(y+y') O5+z particula rly where x is about 0.3 to about 0.5, x' is about 1.5 to about 1.7, y is 0.6, y' is between about 1.0 and 1.4, and where B is Ga or Al. Lax Srx' By Fey' B"2-(y+y') O5+z particula rly where x is about 0.3 to about 0.5, x' is about 1.5 to about 1.7, y is 0.6, y' is between about 1.0 and 1.4, and where B is Ga or Al. Lax Srx' By Fey' Co2-(y+y') O5+z particula rly where x is about 0.3 to about 0.5, x' is about 1.5 to about 1.7, y is 0.6, y' is between about 1.0 and 1.4, and where B is Ga or Al. La0.3 Sr1.7 Ga0.6 Fe1.0-m Com O5+z where m is 0, 0.1, 0.15, 0.20, 0.25, 0.30, 0.35, and 0.40. La0.4 Sr1.6 Ga0.6 Fe1.0-m Com O5+z where m is 0, 0.1, 0.15, 0.20, 0.25, 0.30, 0.35 and 0.40. La0.3 Sr1.7 Al0.6 Fe1.0-m Com O5+z where m is 0, 0.1, 0.15, 0.20, 0.25, 0.30, 0.35 and 0.40. La0.4 Sr1.6 Al0.6 Fe1.0-m Com O5+z where m is 0, 0.1, 0.15, 0.20, 0.25, 0.30, 0.35 and 0.40. La0.3 Sr1.7 Al0.6 Fe1.1 Co0.3 O5+z La0.4 Sr1.6 Al0.6 Fe1.2 Co0.2 O5+z La0.3 Sr1.7 Ga0.6 Fe1.4 O5+z La0.4 Sr1.6 Ga0.6 Fe1.4 O5+z______________________________________
Mixed metal oxide materials of this invention are substantially single-phase in that they are predominately (greater than about 90% by weight) comprised of a single-phase mixed metal oxide of the formula given above. The purity of the materials can be determined by X-ray diffraction methods which are believed to detect the presence of greater than about 4% by weight of other phases. The materials formed on mixing, calcining and milling individual metal oxide powders may contain minor amounts (up to about 10% by weight) of other metal oxides that form distinct phases, but which do not contribute significantly to the electronic and ionic conductivity of the material as a whole. These additional metal oxide phases may be formed unintentionally due to inaccuracies in the amounts of starting materials added because, for example, the starting materials may contain non-volatile impurities (e.g., starting metal oxides may contain low levels of metal carbonates) or volatile impurities (e.g., water) that alter the relative stoichiometries of component metals. Alternatively, additional metal oxide phases may be selectively introduced into the mixed metal oxide material by preparing off-stoichiometric mixtures of starting materials.
FIGS. 1-5 are X-ray diffractometer scans for several mixed metal oxides of the above formula La0.4 Sr1.6 Ga0.6 Fe1.4 O5+z (FIG. 1), La0.3 Sr1.7 Ga0.6 Fe1.1 Co0.3 O5+z (FIG. 2), La0.3 Sr1.7 Al0.6 Fe1.1 Co0.3 O5+z (FIG. 3), La0.4 Sr1.6 Ga0.6 Fe1.2 Co0.2 O5+z (FIG. 4), all of which were calcined, and La0.4 Sr1.6 Al0.6 Fe1.2 Co0.2 O5+z (FIG. 5), calcined and sintered (see Example 1). These scans were run on a Philips PW1830 X-ray generator with model 1050 goniometer for powder samples with a PW3710 control unit. The X-ray diffractometer scans indicate that the mixed metal oxide materials are substantially single-phase oxides of the desired stoichiometry containing small amounts of other oxide phases (less than about 10% by weight). The diffractometer employed can detect greater than about 4% by weight of other phases (as determined by adding increasing amounts of SrAl2 O4 impurity). Small arrows on the scans indicate peaks believed to be indicative of second phases. The shoulder peak at about 32 is believed to be due to (Sr, La)2 AlO4. The peaks between 28-30 are believed to be due to Sr(Fe, Al)2 O4. The peaks at 34 and 41 have not as yet been identified.
In the mixed metal oxides of this invention, Group 2 elements Mg, Ca, Sr, Ba and Ra are believed to be in the 2+ oxidation state. Group 13 elements Al, Ga, and In are believed to be in the 3+ oxidation state. Lanthanides (including lanthanum and yttrium) are believed to be in the 3+ oxidation state. The transition metals in these materials are expected to be of mixed valence (i.e., a mixture of oxidation states) dependent upon the amount of oxygen present and the temperature.
Membranes useful in the oxygen separation method of this invention can be dense, substantially gas impermeable sintered materials in any desired shape, including membrane disks, open tubes, one-open-ended tubes, etc., that can be adapted to form a gas-tight seal between the two zones or chambers discussed above. The membrane can be sealed between the two zone or chambers with a gas tight seal employing approriately selected adhesive or sealant. Membranes can be formed by isostatic pressing of mixed metal oxide materials of this invention into dense substantially gas impermeable membranes. Alternatively, substantially gas-impermeable membranes can be formed by forming dense thin films of ionically and electronically conducting mixed metal oxide on porous substrate materials. Again these two component membranes (porous substrate and dense thin film) can have any desired shape including disks, tubes or one-open-ended tubes. Porous substrates (which allow passage of gas through the substrate) can include various metal oxide materials including metal-oxide stabilized zirconia, titania, alumina, magnesia, or silica, mixed metal oxide materials exhibiting ion and/or electronic conduction or metal alloys, particularly those that minimally react with oxygen. The substrate material should be inert to oxygen or facilitate the desired transport of oxygen. More preferred substrates are those that have a thermal expansion coefficient (over the operational temperatures of the reactor) that is matched to that of the mixed metal oxide ion/electron conducting material.
Thin films (about 10-300 μm thick) of the mixed metal oxides of this invention are formed on the porous substrate by a variety of techniques, including tape casting, dip coating or spin coating. A presently preferred two component membrane is prepared by forming dense thin films of the mixed metal oxides of this invention on a porous substrate formed from the same mixed metal oxide material.
The oxidation and reduction surfaces of the membranes of this invention can optionally be provided with an oxidation catalyst, a reduction catalyst or both. Oxidation and reduction catalysts can be selected from mixed metal oxides having the formula:
Laa A2-a CO2-b Mb O5+a/2+b/2
where 0<b<0.4, 0≦a≦1.6, and where A is Ba, Sr, Ca or mixtures thereof and M is Fe, Cu or Ag or mixtures thereof.
A preferred oxidation/reduction catalyst is La0.8 Sr0.2 CoO3-δ where δ is a number that makes the metal oxide charge neutral. Alternative catalysts include: A2 CO2-b Mb O5+b/2, where 0<b≦0.2, A is Ba, Sr, Ca or mixtures thereof and M is Fe, Ni, Cu, Ag or mixtures thereof; and metals dispersed onto ceramic material, particularly where the metal is Ag, Pd, Pt, Ir, Rh, Ru or mixtures thereof.
Catalysts can be deposited on the membrane surface by any known deposition process. A preferred process is the deposition of the catalysts on the sintered membrane surfaces by spray pyrolysis. Stoichiometric aqueous metal nitrate (or other metal precursor) solutions (having the stoichiometry of the desired metal oxide catalyst, for example, can be spray pyrolyzed by heating to about 700° C. using air as the spray pyrolysis propellant to avoid oxygen depletion during deposition. The pyrolyzed spray is uniformly deposited onto a heated (e.g., to 500° C.) sintered membrane, for example using an air brush device. Other solvents that do not interfere with deposition or react with the catalyst can be employed in the pyrolysis solution. Catalyst loading is varied by adjusting the concentration of the catalyst (or catalyst precursor) in the pyrolysis solution. Catalyst loading will typically be about 0.001 to about 0.1 g/cm2 and preferably about 0.01 gr/cm2.
Starting materials for preparation of mixed metal oxides were obtained from commercial sources and typically were employed without further purification. Higher purity mixed metal oxides can be obtained by initial removal of volatile impurities (e.g., H2 O, by heating starting materials under vacuum). For specific examples below, La2 O3, SrCO3, Ga2 O3, Al2 O3 and Co3 O4 were obtained from Alfa/Aesar at purities indicated below. Fe2 O3 was obtained from Aldrich.
The brownmillerite-derived ceramic materials of this invention were in general prepared from powders using standard solid state synthesis techniques.
A. La0.4 Sr1.6 Ga0.6 Fe1.2 Co0.2 O5+z
The following were combined:
16.34 parts by wt. of La2 O3 (99.9% purity by weight on a rare earth metals basis)
59.23 parts by wt. of SrCO3 (99% purity by weight, with <1% Ba)
14.10 parts by wt. of Ga2 O3 (99.9% purity by weight on a metals basis)
24.03 parts by wt. of Fe2 O3 (99+% purity by weight)
4.03 parts by wt. of Co3 O4 (99.7% purity by weight on a metals basis)
in propanol (about 100 ml) and milled together for 18-24 hrs, after which the milled powder was dried and calcined in an alumina crucible (in air) for 6-12 h at 1175° C.-1250° C. The resulting product was subjected to grinding and sieving before calcining a second time at 1175° C.-1250° C. for 6-12 hrs. X-ray diffraction of calcined powder of La0.4 Sr1.6 Ga0.6 Fe1.2 Co0.2 O5+z shows these materials to be substantially single-phase, containing only small amounts of second phases (<10%), see FIG. 4.
To prepare dense membranes, the resulting powders were mixed with polyvinyl butyral binder and pressed and sintered in air at 1150° C.-1450° C. for 4-12 hours into dense disks and dense open-one-end tubes. Materials containing Ga are preferably sintered at lower temperatures in this range, up to about 1225 ° C. X-ray diffraction of sintered membranes show material to be substantially single-phase containing small amounts (less than about 10%) of second phases.
B. La0.3 Sr1.7 Ga0.6 Fe1.1 C0.3 O5+x was prepared as in A above combining the following starting materials of the same purity and source:
12.40 parts by wt. of La2 O3
63.70 parts by wt. of SrCO3
14.27 parts by wt. of Ga2 O3
22.29 parts by wt. of Fe2 O3
6.11 parts by wt. of Co3 O4
Membranes were prepared as in A above. An X-ray diffraction scan of calcined La0.3 Sr1.7 Ga0.6 Fe1.1 Co0.3 O5+x is provided in FIG. 2.
C. La0.3 Sr1.7 Ga0.6 Fe1.1 Co0.35 O5+x was prepared as in A above combining the following starting materials of the same purity and source:
16.289 parts by wt. of La2 O3
59.044 parts by wt. of SrCO3
14.056 parts by wt. of Ga2 O3
20.597 parts by wt. of Fe2 O3
7.022 parts by wt. of Co3 O4
Membranes were prepared as in A above.
D. La0.4 Sr1.6 Al0.6 Fe1.2 Co0.2 O5+x was prepared as in A above combining the following starting materials of the same purity and source unless otherwise indicated:
17.43 parts by wt. of La2 O3
63.17 parts by wt. of SrCO3
8.18 parts by wt. of αAl2 O3 (alpha-alumina)(99.9% purity by weight on a metals basis)
25.62 parts by wt. of Fe2 O3
4.29 parts by wt. of Co3 O4
Dense membranes were prepared as described above in A with the exception that materials containing Al are preferably sintered at temperatures at the higher end of the range given, i.e. at about 1300° C. or above and preferably at 1400° C. to 1420° C. An X-ray diffraction scan of sintered material is provided in FIG. 5.
An open-one-end membrane tube (about 1.0 mm m thick) prepared from La0.3 Sr1.7 Ga0.6 Fe1.1 Co0.35 O5+x as described in Example 1 C was incorporated into a membrane reactor with a Pyrex seal used to isolate the air from the permeate chamber. A slurry of La0.8 Sr0.2 CoO3-x (in 1, 2-butanediol) was applied on both the anode (oxidation) and cathode (reduction) sides of the membrane to serve as both oxidation and reduction catalysts. Gas flows on both sides of the membrane were under ambient pressure. Air flow on the cathode side of the reactor was held at 600 ml/min, and the He flow on the anode side was fixed at 400 ml/min. Under these conditions, an oxygen flux of 0.9 ml/min-cm2 was maintained at 900° C. for 700 h of operation. This is equivalent to an oxygen ion conductivity of 0.7 S/cm. An activation energy of less than 0.5eV was calculated from temperature dependent measurements. Oxygen conductivity is calculated from oxygen flux (or permeation) according to the equation:
J is the oxygen permeation in ml/min-Cm3,
d is membrane thickness in cm,
T is temperature in K,
P' and P" are the oxygen partial pressures on opposite sides of the membrane.
See, Y. Teraoka, et al. (1988) Mater. Res. Bull. 23:51.
Table 1 provides oxygen permeation data for dense membranes (about 0.8-1.0 mm thick) prepared by isostatic pressing of mixed metal oxide materials of this invention. Membranes were prepared as open-one-ended tubes. In these experiments, the partial pressure of oxygen on the cathode side was 0.21 atm (O2 in air) and on the anode side was maintained at 0.02 atm. He flow on the anode side was adjusted to maintain the constant oxygen partial pressure of 0.02 atm. In both cases gas flows were at ambient pressure. Maintenance of the constant partial pressures of oxygen on either side of the membrane allows comparison of data among different membrane materials.
Table 1 also lists ion conductivities which are calculated using the equation above. The values of oxygen permeation and calculated conductivity given in the table at those measured after operation in a reactor for the time listed in Table 1. FIGS. 6 and 7 are graphs comparing oxygen flux or permeation (ml/min-cm2) as a function of time at 900° C. for several different membrane materials. FIG. 6 compares oxygen flux as a function of time using membranes prepared from La0.3 Sr1.7 Ga0.6 Fe1.4-y Coy O5+z where 0.0≦y<0.4, indicating that the amount of Co is varied. The preferred material over time based on this data is that where y=0.30. FIG. 7 compares oxygen flux as a function of time using membranes prepared from La0.4 Sr1.6 Ga0.6 Fe1.4-y Coy O5+z where 0.0<y<0.4, indicating that the amount of Co is varied. The preferred material over time based on these data is that where y=0.20.
Membranes for oxygen separation reactors can be prepared by coating a substrate with a thin film (about 10-about 300 μm thick) of a mixed metal oxide material of this invention. In particular a porous substrate material can be coated with a dense thin film of these materials to provide a substantially gas impermeable membrane. In general, thin films are applied to selected substrates by methods known in the art, including tape casting, dip coating or spin coating. Presently preferred thin film-coated membranes are prepared using a porous membrane as a substrate where the porous membrane is made of a mixed metal oxide of the same or similar composition to the ion and electron conduction mixed metal oxide that will comprise the thin film. Use of a substrate that has the same or a similar (preferably within about 20% of) thermal expansion coefficient as the thin film material will minimize or avoid cracking of the film and/or membrane on heating. Furthermore, use of a chemically similar material for both the substrate and thin film will minimize undesired reactivity of the two materials with each other and undesired reactivity of the substrate with gases in the reactor. Porous membranes of the mixed metal oxides of this invention can be prepared in a variety of ways, for example, by combining the metal oxide with an organic filler (up to about 20% by weight), such as cellulose or starch particles of a selected size range 9 e.g. about 20 μm particles), shaping or pressing the desired membrane and sintering. The organic filler is destroyed and removed on sintering leaving desired pores of a selected size in the membrane. Thin films are preferably uniformly thick and crack-free on firing. Uniform deposition of films can for example be obtained by use of colloidal suspensions of the metal oxide in a selected solvent. The suspension is applied to the porous substrate by conventional coating or casting methods to give a uniform deposition which on firing gives a film of uniform thickness. An alternative method for applying thin films is the use of co-polymeric precursors which comprise metal oxide incorporated into the polymer. Flat membranes or tubular membranes can be prepared having dense thin films of the metal oxide mixed ion and electron conductors of this invention.
Those of ordinary skill in the art will appreciate that methods, materials, reagents, solvents, membrane structures and reactors other than those specifically described herein can be employed or adapted without undue experimentation to the practice of this invention. All such variants in methods, materials, reagents, solvents, structures and reactors that are known in the art and that can be so adapted or employed are encompassed by this invention.
TABLE 1__________________________________________________________________________ total J (ml/min-cm2) σion (S/cm) time Temperature (° C.) Temperature (° C.)Membrane Compound (hr) 750 800 850 900 Ea 750 800 850 900 Ea__________________________________________________________________________Sr1.6 La0.4 Ga0.6 Fe1.3 Co0.1 O5+z 144 0.092 0.138 0.207 0.231 0.66 0.033 0.053 0.088 0.098 0.79 Sr1.6 La0.4 Ga0.6 Fe1.25 Co0.15 O5+z 144 0.327 0.447 0.600 0.725 0.56 0.140 0.201 0.285 0.352 0.64 Sr1.6 La0.4 Ga0.6 Fe1.2 Co0.2 O5+z 168 0.529 0.778 1.023 1.282 0.61 0.213 0.339 0.470 0.616 0.73 Sr1.6 La0.4 Ga0.6 Fe1.15 Co0.25 O5+z 168 0.201 0.289 0.560 0.793 0.99 0.057 0.084 0.185 0.277 1.14 Sr1.6 La0.4 Ga0.6 Fe1.1 Co0.3 O5+z 360 0.297 0.456 0.629 0.882 0.74 0.098 0.160 0.229 0.340 0.84 Sr1.6 La0.4 Ga0.6 Fe1.05 Co0.35 O5+z 168 0.226 0.355 0.700 1.184 1.17 0.069 0.114 0.261 0.507 1.40 Sr1.7 La0.3 Ga0.6 Fe1.3 Co0.1 O5+z 168 0.164 0.246 0.363 0.523 0.80 0.061 0.094 0.147 0.224 0.90 Sr1.7 La0.3 Ga0.6 Fe1.2 Co0.2 O5+z 192 0.035 0.059 0.074 0.141 0.91 0.008 0.014 0.018 0.038 1.00 Sr1.7 La0.3 Ga0.6 Fe1.15 Co0.25 O5+z 144 0.124 0.188 0.286 0.394 0.81 0.054 0.086 0.142 0.212 0.95 Sr1.7 La0.3 Ga0.6 Fe1.1 Co0.3 O5+z 192 0.298 0.508 0.888 1.239 1.00 0.101 0.190 0.379 0.570 1.22 Sr1.7 La0.3 Ga0.6 Fe1.05 Co0.35 O5+z 168 0.146 0.228 0.325 0.484 0.82 0.059 0.101 0.156 0.266 1.02 Sr1.7 La0.3 Ga0.6 Fe1.4 O5+z 192 0.343 0.487 0.625 0.751 0.54 0.143 0.217 0.291 0.361 0.64__________________________________________________________________________
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US3607863 *||28 Feb 1967||21 Sep 1971||Dyckerhoff Zementwerke Ag||Clathrate compounds|
|US3754951 *||26 Jul 1971||28 Aug 1973||Kaiser Aluminium Chem Corp||Periclase refractory grain|
|US4083730 *||20 Jul 1976||11 Apr 1978||Perlmooser Zementwerke A.G.||Cement, process and device for its production|
|US4330633 *||3 Feb 1981||18 May 1982||Teijin Limited||Solid electrolyte|
|US4791079 *||9 Jun 1986||13 Dec 1988||Arco Chemical Company||Ceramic membrane for hydrocarbon conversion|
|US4793904 *||5 Oct 1987||27 Dec 1988||The Standard Oil Company||Process for the electrocatalytic conversion of light hydrocarbons to synthesis gas|
|US4802958 *||17 Mar 1987||7 Feb 1989||The Standard Oil Company||Process for the electrocatalytic oxidation of low molecular weight hydrocarbons to higher molecular weight hydrocarbons|
|US4827071 *||15 Jun 1988||2 May 1989||Arco Chemical Technology, Inc.||Ceramic membrane and use thereof for hydrocarbon conversion|
|US4933054 *||13 Mar 1987||12 Jun 1990||The Standard Oil Company||Electrocatalytic oxidative dehydrogenation of saturated hydrocarbons to unsaturated hydrocarbons|
|US5160618 *||2 Jan 1992||3 Nov 1992||Air Products And Chemicals, Inc.||Method for manufacturing ultrathin inorganic membranes|
|US5160713 *||9 Oct 1990||3 Nov 1992||The Standard Oil Company||Process for separating oxygen from an oxygen-containing gas by using a bi-containing mixed metal oxide membrane|
|US5210059 *||10 Oct 1991||11 May 1993||Exxon Research & Engineering Company||Multilayered catalyst for controlled transport of reactant|
|US5240473 *||1 Sep 1992||31 Aug 1993||Air Products And Chemicals, Inc.||Process for restoring permeance of an oxygen-permeable ion transport membrane utilized to recover oxygen from an oxygen-containing gaseous mixture|
|US5240480 *||15 Sep 1992||31 Aug 1993||Air Products And Chemicals, Inc.||Composite mixed conductor membranes for producing oxygen|
|US5306411 *||27 Nov 1990||26 Apr 1994||The Standard Oil Company||Solid multi-component membranes, electrochemical reactor components, electrochemical reactors and use of membranes, reactor components, and reactor for oxidation reactions|
|US5356728 *||16 Apr 1993||18 Oct 1994||Amoco Corporation||Cross-flow electrochemical reactor cells, cross-flow reactors, and use of cross-flow reactors for oxidation reactions|
|US5366712 *||3 Feb 1993||22 Nov 1994||Enea-Ente Per Le Nuove Tecnologie, L'energia E L'ambiente||Ceramic catalytic membrane reactor for the separation of hydrogen and/or isotopes thereof from fluid feeds|
|US5393325 *||8 Nov 1993||28 Feb 1995||Bend Research, Inc.||Composite hydrogen separation metal membrane|
|US5397541 *||10 Sep 1993||14 Mar 1995||National Research Council Of Canada||Thin film oxygen sensor|
|US5430209 *||27 Aug 1993||4 Jul 1995||Mobil Oil Corp.||Process for the catalytic dehydrogenation of alkanes to alkenes with simultaneous combustion of hydrogen|
|US5466646 *||18 Aug 1992||14 Nov 1995||Worcester Polytechnic Institute||Process for the preparation of solid state materials and said materials|
|US5534471 *||12 Jan 1994||9 Jul 1996||Air Products And Chemicals, Inc.||Ion transport membranes with catalyzed mixed conducting porous layer|
|US5569633 *||12 Jan 1994||29 Oct 1996||Air Products And Chemicals, Inc.||Ion transport membranes with catalyzed dense layer|
|US5591315 *||24 Feb 1995||7 Jan 1997||The Standard Oil Company||Solid-component membranes electrochemical reactor components electrochemical reactors use of membranes reactor components and reactor for oxidation reactions|
|US5639437 *||3 Sep 1996||17 Jun 1997||Amoco Corporation||Oxygen ion-conducting dense ceramic|
|US5648304 *||13 Mar 1996||15 Jul 1997||Mazanec; Terry J.||Oxygen permeable mixed conductor membranes|
|US5693212 *||15 Aug 1996||2 Dec 1997||The Standard Oil Company||Solid multi-component membranes, electrochemical reactor components, electrochemical reactors and use of membranes, reactor components, and reactor for oxidation reactions|
|US5702999 *||10 Dec 1996||30 Dec 1997||The Standard Oil Company||Oxygen permeable mixed conductor membranes|
|US5712220 *||29 Feb 1996||27 Jan 1998||Air Products And Chemicals, Inc.||Coompositions capable of operating under high carbon dioxide partial pressures for use in solid-state oxygen producing devices|
|US5714091 *||7 Jun 1995||3 Feb 1998||The Standard Oil Company||Process for the partial oxydation of hydrocarbons|
|US5723035 *||7 Jun 1995||3 Mar 1998||The Standard Oil Company||Coated membranes|
|US5744015 *||7 Jun 1995||28 Apr 1998||Mazanec; Terry J.||Solid multi-component membranes, electrochemical reactor components, electrochemical reactors and use of membranes, reactor components, and reactor for oxidation reactions|
|US5779904 *||7 Jun 1995||14 Jul 1998||Inrad||Synthesis of inorganic membranes on supports|
|US5788748 *||20 Dec 1995||4 Aug 1998||The Standard Oil Company||Oxygen permeable mixed conductor membranes|
|US5817597 *||29 Feb 1996||6 Oct 1998||Air Products And Chemicals, Inc.||Compositions capable of operating under high oxygen partial pressures for use in solid-state oxygen producing devices|
|US5821185 *||21 Jun 1995||13 Oct 1998||Eltron Research, Inc.||Solid state proton and electron mediating membrane and use in catalytic membrane reactors|
|US6010614 *||3 Jun 1998||4 Jan 2000||Praxair Technology, Inc.||Temperature control in a ceramic membrane reactor|
|US6056807 *||26 Jan 1998||2 May 2000||Air Products And Chemicals, Inc.||Fluid separation devices capable of operating under high carbon dioxide partial pressures which utilize creep-resistant solid-state membranes formed from a mixed conducting multicomponent metallic oxide|
|EP0399833A1 *||24 May 1990||28 Nov 1990||The Standard Oil Company||Novel solid multi-component membranes, electrochemical reactor and use of membranes and reactor for oxidation reactions|
|EP0438902B1 *||20 Dec 1990||7 May 1997||The Standard Oil Company||Electrochemical reactors and multicomponent membranes useful for oxidation reactions|
|EP0673675A2 *||24 May 1990||27 Sep 1995||The Standard Oil Company||Solid multi-component membranes for reactions|
|EP0705790A1 *||21 Sep 1995||10 Apr 1996||The Standard Oil Company||Oxygen permeable mixed conductor membranes|
|EP0766330A1 *||20 Dec 1990||2 Apr 1997||The Standard Oil Company||Components for use in electrochemical cells and their use in oxygen separation|
|GB2203446A *||Title not available|
|WO1994024065A1 *||5 Apr 1994||27 Oct 1994||Amoco Corporation||Oxygen ion-conducting dense ceramic|
|WO1997041060A1 *||13 Sep 1996||6 Nov 1997||Eltron Research, Inc.||Solid state oxygen anion and electron mediating membrane and catalytic membrane reactors containing them|
|1||*||Chick et al. (1990)Mater. Lett. 10(1,2):6 12.|
|2||Chick et al. (1990)Mater. Lett. 10(1,2):6-12.|
|3||*||Cook et al. (1990) J. Electrochem. Soc. 137:3309 3310.|
|4||Cook et al. (1990) J. Electrochem. Soc. 137:3309-3310.|
|5||*||Cook, R.L. and Sammells, A.F. (1991) Solid State Ionics 45:311 321.|
|6||Cook, R.L. and Sammells, A.F. (1991) Solid State Ionics 45:311-321.|
|7||*||Crespin, M. and Hall, K.W. (1981) J. Catal. 69:359 370.|
|8||Crespin, M. and Hall, K.W. (1981) J. Catal. 69:359-370.|
|9||*||Gallagher et al. (1964) J. Chem. Phys. 41(8):2429 2434.|
|10||Gallagher et al. (1964) J. Chem. Phys. 41(8):2429-2434.|
|11||*||Goodenough et al. (1990) Solid State Ionics 44:21 31.|
|12||Goodenough et al. (1990) Solid State Ionics 44:21-31.|
|13||*||Greaves et al. (1975) Acta Cryst. B31:641 646.|
|14||Greaves et al. (1975) Acta Cryst. B31:641-646.|
|15||*||Hawley s Condensed Chemical Dictionary. 13th Ed., revised by Richard J Lewis Sr., John Wiley & Sons, Inc. USA, ISBN 0 471 29205 2, p. 852, 1997.|
|16||Hawley's Condensed Chemical Dictionary. 13th Ed., revised by Richard J Lewis Sr., John Wiley & Sons, Inc. USA, ISBN 0-471-29205-2, p. 852, 1997.|
|17||*||Kuchynka, D.J. et al. (1991) J. Electrochem. Soc. 138(5):1284 1299.|
|18||Kuchynka, D.J. et al. (1991) J. Electrochem. Soc. 138(5):1284-1299.|
|19||*||Matsumoto et al. (1980) J. Electrochem. Soc. 127(11):2360 2364.|
|20||Matsumoto et al. (1980) J. Electrochem. Soc. 127(11):2360-2364.|
|21||*||Pederson et al. (1991) Mater. Lett. 10(9,10):437 443.|
|22||Pederson et al. (1991) Mater. Lett. 10(9,10):437-443.|
|23||*||Pujare, N U and Sammells, A.F. (1988) J. Electrochem. Soc. 135(10):2544 2545.|
|24||Pujare, N U and Sammells, A.F. (1988) J. Electrochem. Soc. 135(10):2544-2545.|
|25||*||Rostrup Nielson, J.R. and Bak Hansen, J. H. (1993) J. Catalysis 144:38 49.|
|26||Rostrup-Nielson, J.R. and Bak Hansen, J.-H. (1993) J. Catalysis 144:38-49.|
|27||*||Sammells et al. (1992) Solid State Ionics 52:111 123.|
|28||Sammells et al. (1992) Solid State Ionics 52:111-123.|
|29||Sammells, A.F. and Cook, R.L. (1991), "Rational Selection of Advanced Solid Electrolytes for Intermediate Temperature Fuel Cells," presented at the Ceramic Conductors for Solid-State Electrochemical Devices Meeting, May 12-15, 1991, Snowbird, UT, (abstract only).|
|30||*||Sammells, A.F. and Cook, R.L. (1991), Rational Selection of Advanced Solid Electrolytes for Intermediate Temperature Fuel Cells, presented at the Ceramic Conductors for Solid State Electrochemical Devices Meeting, May 12 15, 1991, Snowbird, UT, (abstract only).|
|31||Sammells, T., (1991), "Rational Selection of Perovskites for Solid Electrolytes and Electrocatalysis," Presented at BP America Research, Warrenville Research Center, Sep. 16, 1991, 46pp.|
|32||*||Sammells, T., (1991), Rational Selection of Perovskites for Solid Electrolytes and Electrocatalysis, Presented at BP America Research, Warrenville Research Center, Sep. 16, 1991, 46pp.|
|33||*||Schwartz, M. et al. (1993) J. Electrochem. Soc. 140(4):L62 L63 (Apr.).|
|34||Schwartz, M. et al. (1993) J. Electrochem. Soc. 140(4):L62-L63 (Apr.).|
|35||*||Shin, S. and Yonemura, M. (1978) Mat. Res. Bull. 13:1017 1021.|
|36||Shin, S. and Yonemura, M. (1978) Mat. Res. Bull. 13:1017-1021.|
|37||*||Teraoka et al. (1985) Chem. Lett. 1367 1370.|
|38||Teraoka et al. (1985) Chem. Lett. 1367-1370.|
|39||*||Teraoka et al. (1985) Chem. Lett. 1743 1746, The Chemical Society of Japan.|
|40||Teraoka et al. (1985) Chem. Lett. 1743-1746, The Chemical Society of Japan.|
|41||*||Teraoka et al. (1988) Chem. Lett. 503 506, The Chemical Society of Japan.|
|42||Teraoka et al. (1988) Chem. Lett. 503-506, The Chemical Society of Japan.|
|43||*||Teraoka et al. (1988) Mat. Res. Bull. 23:51 58.|
|44||Teraoka et al. (1988) Mat. Res. Bull. 23:51-58.|
|45||*||Teraoka, Y. et al. (1989) J. Ceram. Soc. Jpn. Inter. Ed. 97:458 462.|
|46||Teraoka, Y. et al. (1989) J. Ceram. Soc. Jpn. Inter. Ed. 97:458-462.|
|47||*||Teraoka, Y. et al. (1989) J. Ceram. Soc. Jpn. Inter. Ed. 97:523 529.|
|48||Teraoka, Y. et al. (1989) J. Ceram. Soc. Jpn. Inter. Ed. 97:523-529.|
|49||*||van der Pauw (1958) Philips Res. Rep. 13(1):1 9.|
|50||van der Pauw (1958) Philips Res. Rep. 13(1):1-9.|
|51||*||Zhen, Y.S. and Goodenough, J.B. (1990) Mat. Res. Bull. 25:785 790.|
|52||Zhen, Y.S. and Goodenough, J.B. (1990) Mat. Res. Bull. 25:785-790.|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US6352955 *||22 Jun 1999||5 Mar 2002||Catalytic Solutions, Inc.||Perovskite-type metal oxide compounds|
|US6361584 *||2 Nov 1999||26 Mar 2002||Advanced Technology Materials, Inc.||High temperature pressure swing adsorption system for separation of oxygen-containing gas mixtures|
|US6372686 *||10 Nov 2000||16 Apr 2002||Catalytic Solutions, Inc.||Perovskite-type metal oxide compounds and methods of making and using thereof|
|US6471921 *||19 May 1999||29 Oct 2002||Eltron Research, Inc.||Mixed ionic and electronic conducting ceramic membranes for hydrocarbon processing|
|US6503296 *||5 Jun 1998||7 Jan 2003||Norsk Hydro Asa||Membrane and use thereof|
|US6514314 *||4 Dec 2000||4 Feb 2003||Praxair Technology, Inc.||Ceramic membrane structure and oxygen separation method|
|US6524421 *||22 Sep 2000||25 Feb 2003||Praxair Technology, Inc.||Cold isopressing method|
|US6531425||4 Dec 2001||11 Mar 2003||Catalytic Solutions, Inc.||Catalytic converter comprising perovskite-type metal oxide catalyst|
|US6592782 *||22 Dec 2000||15 Jul 2003||Eltron Research, Inc.||Materials and methods for the separation of oxygen from air|
|US6641626 *||19 Sep 2002||4 Nov 2003||Eltron Research, Inc.||Mixed ionic and electronic conducting ceramic membranes for hydrocarbon processing|
|US6786952 *||22 Sep 2000||7 Sep 2004||Norsk Hydro Asa||Membrane and use thereof|
|US6949230||14 Aug 2001||27 Sep 2005||Eltron Research, Inc.||Solid state oxygen anion and electron mediating membrane and catalytic membrane reactors containing them|
|US7014825||6 Feb 2003||21 Mar 2006||Catalytic Solutions, Inc.||Perovskite-type metal oxide compounds and methods of making and using thereof|
|US7387755 *||21 Mar 2005||17 Jun 2008||Praxair Technology, Inc.||Method of making a ceramic composite|
|US7514055||20 Sep 2005||7 Apr 2009||Catalytic Solutions, Inc.||Method of controlling emissions from a diesel cycle internal combustion engine with perovskite-type metal oxide compounds|
|US7866486||23 Jan 2006||11 Jan 2011||Uhde Gmbh||Composite ceramic hollow fibres method for production and use thereof|
|US8435920 *||7 May 2013||Eltron Research & Development, Inc.||Cyclic catalytic upgrading of chemical species using metal oxide materials|
|US20020054845 *||14 Aug 2001||9 May 2002||Michael Schwartz||Solid state oxygen anion and electron mediating membrane and catalytic membrane reactors containing them|
|US20030059351 *||19 Jul 2002||27 Mar 2003||National Inst. Of Advanced Ind. Science And Tech.||Chemical reactor|
|US20030198582 *||6 Feb 2003||23 Oct 2003||Catalytic Solutions, Inc.||Perovskite-type metal oxide compounds and methods of making and using thereof|
|US20060109453 *||20 Sep 2005||25 May 2006||Swift David R||Apparatuses and methods for measuring head suspensions and head suspension assemblies|
|US20060127656 *||2 Feb 2005||15 Jun 2006||Gallo Pascal D||Catalytic membrane reactor|
|US20060208377 *||21 Mar 2005||21 Sep 2006||Chen Jack C||Method of making a ceramic composite|
|US20070140933 *||25 Aug 2006||21 Jun 2007||Bp Corporation North America Inc.||Membrane Systems Containing An Oxygen Transport Membrane And Catalyst, And Methods Of Using The Same|
|US20090061278 *||26 Aug 2008||5 Mar 2009||Mohan Menon||Polymerized inorganic-organic precursor solutions and sintered membranes|
|US20110024687 *||3 Feb 2011||Eltron Research & Development, Inc.||Cyclic catalytic upgrading of chemical species using metal oxide materials|
|EP1412053A1 *||3 Jul 2002||28 Apr 2004||Advanced Technology Materials, Inc.||Method for carbon monoxide reduction during thermal/wet abatement of organic compounds|
|WO2006061390A1||6 Dec 2005||15 Jun 2006||L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude||Catalytic membrane reactor|
|U.S. Classification||423/219, 502/4, 55/524, 95/54, 96/4|
|International Classification||C01B13/02, B01J19/00, B01J23/83, B01D53/32, B01J19/24, B01J35/00, B01J8/00, B01J12/00, C01B3/36, C01B17/04, B01D53/22, B01J23/00, B01D71/02, H01M8/12, B01J4/04, C01C3/02, B01J35/06, C01B3/38|
|Cooperative Classification||H01M8/1231, B01J2219/00063, C01B2203/1041, Y02E60/525, B01J12/007, C01B2203/1035, H01M8/1246, B01D53/228, Y02E60/521, C01B2203/1064, C01B17/0465, B01D53/326, C01B2203/1011, H01M4/9033, C01B3/36, B01J23/002, H01M4/9066, B01J35/0033, B01D2325/18, B01D2325/10, B01J2219/00051, B01J8/009, B01J2219/00189, B01J2219/0018, C01B2203/1082, C01B3/386, B01J19/2475, C01C3/0216, B01J35/065, B01D69/141, B01J2208/00601, B01D2323/12, B01D67/0041, C01B2210/0046, B01D2323/08, B01D71/024, C01B2203/1258, C01B2203/1052, C01B13/0255, C01B2203/1241, B01J23/83, C01B2203/0261, B01J2523/00, Y02P70/56|
|European Classification||B01D67/00M10, B01D69/14B, B01J12/00P, H01M8/12B, B01D71/02P, B01J23/83, B01D53/22M, B01J19/24P, B01D53/32E, C01B17/04B14D, H01M8/12E2, C01B3/36, B01J8/00L4, C01B13/02D4B2, C01C3/02D1B, B01J35/06B, B01J35/00D4, B01J23/00B, C01B3/38D|
|21 Apr 1999||AS||Assignment|
Owner name: ELTRON RESEARCH, INC., COLORADO
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:MACKAY, RICHARD;SCHWARTZ, MICHAEL;SAMMELLS, ANTHONY F.;REEL/FRAME:009897/0738
Effective date: 19990412
|28 Dec 2000||AS||Assignment|
Owner name: ENERGY, U.S. DEPARTMENT OF, CALIFORNIA
Free format text: CONFIRMATORY LICENSE;ASSIGNOR:ELTRON RESEARCH INC.;REEL/FRAME:011385/0566
Effective date: 20000310
|13 Nov 2001||CC||Certificate of correction|
|16 Mar 2004||FPAY||Fee payment|
Year of fee payment: 4
|26 Jun 2008||FPAY||Fee payment|
Year of fee payment: 8
|26 Nov 2008||AS||Assignment|
Owner name: GUARANTY BANK, COLORADO
Free format text: SECURITY INTEREST;ASSIGNOR:ELTRON RESEARCH, INC.;REEL/FRAME:021924/0143
Effective date: 20050620
|6 Aug 2012||REMI||Maintenance fee reminder mailed|
|26 Dec 2012||LAPS||Lapse for failure to pay maintenance fees|
|12 Feb 2013||FP||Expired due to failure to pay maintenance fee|
Effective date: 20121226